Conversion of olefins, carbon monoxide, and hydrogen



Aug. 12, 1952 B. 1.. EVER'ING ET AL 2,606,939

CONVERSION OF OLEFINS, cmgou MONOXIDE, AND HYDROGEN Filed June 25. 1949 7 Sheets-Sheet 1 TEMPERATURE C H in Product CH In Product 0 in Product 0 Wt. 2 Conversion 0 H Wt. 70

O Wt 7;

E1 Wt. 75

' O O o o o 0 Q 00 w m V lNBOHBd .LH9I3M 1-3 INVENTORS:

Bernard L. Evering 2 Edwin F. Peters EL A TTORNE Y Aug. 12, 1952 B. L.E\ IERING El AL 2,606,939

CONVERSION OF QLEFINS, CARBON MONUXIDE, AND HYDROGEN Filed June 25, 1949 7 Sheets-Sheet 2 O 0 no 8 0 f" B\ qx \o v o O 8 i u II D E n:

U N :E g g a '88? c a. i it c' I: g N s S I Q. O c I Q 8 60 6" 84 N N N 1% O 0 v Q o O Q 8 r o .LN3QH3d lHSIBM INVENTORS:

Bernard L. Evering Edwin F Pefers ATTORNEY Filed June 25, 1949 7 Sheets-Sheet 3 O O m o g X J It] x L m B G 6 aw 0 2 E 0 Q q n. n. E g '3 s s .s a k k 3%; 8 o w I n o Q Q Q Q Q N N N N M O X 0 U B .LNBOHBd .LH9I3M INVENTORS. (9 "Bernard L. Evering H Edwin F. Peters IL Aug. 12, 1952 B. EVERING El AL 2,606,939

CONVERSION OF OLEFINS, CARBON MONOXIDE, AND HYDROGEN A TTORNE Y Aug. 12, 1952 B. EVERING ET AL 2,606,939

CONVERSION OF OLEFINS, CARBON MONOXIDE, AND HYDROGEN Filed June 25, 1949 7 Sheets-Shes 4 l-Ll I D 0: LLI o 0 g o Q 8 8 a? s Q. t 1 .s t s c L $1 N a 8 g n I g Q g u o o o N N N as 5' 5 27' olx o e D l Q g a 8 2 a O .LNBOUBd .LH9I3M q zzvmvrogs: Bernard L. Evermg H Edwin F. Peters L ATTORNEY Aug. 12, 1952 B. EVERING ET AL CONVERSION OF OLEFINS, CARBON MONOXIDE, AND HYDROGEN Filed June 25, 1949 7 Sheets-Sheet 5 6. umnbumzmh 00 com com 09 o X l o A 4 x ow O Ow t $35.5 M e on 5.59.5 N a 1 teusm 5 +8 N i u \UDUOMQ pi QIU N O .2! uabonl 5 QI NO N, .t: x t o 5.5950 N 0 IINVENITORS Bernard L. Evering Edwin F. Peters A TTORNE Y Aug. 12, 1952 B. L. EVERING ET AL CONVERSION OF OLEF'INS, CARBON MONOXIDE, AND HYDROGEN Filed June 25, 1949 7 Sheets-Sheet '7 3x330 cmmt mokqmmzmumm N\.\ T WW MNR U,./mm y a Y mm 4/ SEE mztqm mmm B mokwzoto mm (vm mo mummommq QEQEE mm mm mw I DD km INVENTORS: Bernard L. Evering Edwin F. Peters BY: d 6 Q N wwm ATTORNEY ence of catalysts comprising iron as the Patented Aug. 12, 1952 CONVERSION OF oL FINs, CARBON 7 MONQXIVDE, ANDHYDROGEN} Bernard L.---Evering and Edwin F. Peters, Chicago,

111., assignors to Standard Oil Company, Chi-, page, 111., a corporation of Indiana Application June 25, 1949, Serial No. 101,462

9 Claims. (Cl. 260. 683J) This invention relates to a novel method for the conversion of olefins in the presence of catalysts containing iron as an essential component. More particularly, it relates to a process for the conversion of mono-olefinic hydrocarbons to hydrocarbons, particularly olefins containing a greater number of carbon atoms per molecule than the olefinic feed stock, by processing said feed stock with carbon monoxide and hydrogen in the presprincipal component.

Some study has heretofore been devoted to the possibility of using iron catalysts to polymerize or otherwise convert mono-olefinic hydrocarbons, particularly ethylene, to higher hydrocarbons in the presence of iron catalysts. These studies led to the conclusions that iron catalysts exhibited little or none of the desired catalytic activity and their use led merely to rapid decomposition of the olefinic charging stock to produce hydrogen and carbon, resulting in rapid fouling of the catalyst and reaction tubes (H. W. Walker, J. Phys. Chem. 31, 961-996 (1927), especially pages 987, 992 and 993). The treatment of ethylene with hydrogen in the presence of iron catalysts has been shown to yield large proportions of methane and ethane, along with some liquid olefin polymers (Y. N. Ipatieif, Catalytic Reactions at High Pressures and Temperatures, Macmillan (30., N. Y., 1936, pp. 113-118). A previous attempt to eifect interaction between ethylene, carbon monoxide and hydrogen in the presence of an iron-copper catalyst resulted in no conversion of the ethylene, although the carbon monoxide and hydrogen participated in a Fischer-Tropsch reaction (Smith, Hawk and Golden, J. Am. Chem. Soc. 52, 3221 (1930), especially pages 3229 and 3230).

One object of our invention is to provide a process utilizing catalysts comprising essentially iron for the conversion of olefinic hydrocarbons to hydrocarbons, particularly olefins, containing a greater number of carbon atoms per molecule than the olefinic feed stock. Another object of our invention is to provide a process for the polymerization and/or hydropolymerization of monoolefinic hydrocarbons in the presence-of catalysts .comprising essentially iron under conditions which maximize the formation of the desired hydrocarbon conversion products and minimize the production of hydrogen and carbon. v v

Still another. object of our invention .is toprovide a process for the conversion of normally gaseous olefins, particularly non-tertiary olefins, to hydrocarbon products, of higher, molecular weight and predominantly straight chain structure by treatment Withcarbon monoxide and hydrogen under selectedv operating. conditions in the presence of catalysts. comprising essentially iron. Alfurtherobjectof our invention isto PIO- vide methods for increasing the life of catalysts comprising essentiallyi'iron during" conversion of mono-olefinic hydrocarbonsfin their presence. These and otherjobjectsof our invention will'be apparent from the ensuing description thereof,

read in connection with the appendedfigur'es.

Briefly, the. present invention relates to a process for the simultaneous conversion of olefinic hydrocarbons, particularly, normally gaseous, non-tertiary olefins, carbon monoxide and hydrogen to producepredominantly hydrocarbon products containing a greater number of carbon atoms per'molecule thanthe olefinic charging stock in the presence of iron-type catalysts under selected operating conditions under which uncontrolled decomposition of the'charging stock to produce principally carbon and hydrogenjis substantially averted. I 1 The process of our invention will-be readily understood by'r'eference to the following specific examples'which are intended to be illustrative bu not unduly limitative. g

- T Figure 1' graphically presents information obtained by polymerizing ethylene in the presence of a reduced'iron catalyst at various temperatures 'anda reaction pressure Sf 1100 p. s. i. g'. It"will be'n'oted from this figure-and'the tabulated data below that substantial conversion of ethylene was short catalyst life could be expected in this operacbtained particularly at "temperatures between about 450 and"600" *C] In this temperature range, considerable production of methane was evident. Also, it appeared that onlya relatively Figure 2 graphically presents yield and conversion information obtained by treatment of ethylene at various temperatures, and a pressure of 720 p. s. i. g. in the presence of a reduced iron catalyst containing about 0.5 weight percent K20. It will be noted by comparison with Figure 1 that the alkalized iron catalyst was somewhat more active than iron alone, the rate of ethylene conversion increasing rapidly to a value between 74 and 78 weight percent 'at a temperature of about 400 C. It will be noted, however, that the catalyst functions principally to convert ethylene to ethane by hydrogen transfer, especially under conditions of' substantial conversion of the ethylene feed stock; Thus, it will be noted'that at about 400 C. substantial conversion of ethylene was obtained but that the reaction of hydrogen transfer predominated over the. conversion. of ethylene to hydrocarbon productscontaining three or more carbon atoms per molecule.

Figure 3 presents information obtained by charging carbon monoxide with ethylene over an alkalized iron catalyst containing 0.5 weight percent of K20 at 1000 p. s. i. g. and various'temperatures. It will be noted from Figure 3 and the following tabulated data that ethylene conversion increased rapidly at about 350 C. from avalue of about 12 to 100% at 390 C. However, in the'temperature' range in which substantial ethylene conversion 'was'being" obtained, the undesirablerea'ction of hydrogen transfer to produce'e'thane was likewise proceeding substantially,

, i.. e. to the extent of producing about '25 to 40 weight percent of ethane'in'the product stream. It will. also be noted from Figure 3 and the tabulateddata' that increased ethylene conversion coincided with a marked decrease in the production of C3 and higher molecular weight hydrocarbons- Although carbon monoxide conversion was essentially quantitative at temperatures between about 300and 400 0., it will be noted that the presence of carbon monoxide did not desirably afiect the product distribution.

.cent) was effected over an alkalized iron catalyst at 1200 p. s. i. gand temperatures varying between 120- and 417 C. Although extensive conversion of ethyleneoccuried in the temperature interval of 350 to- 400 C., it will. be noted from the curves in Figure 4 and by the supporting data in the table that the sin le predominating reaction resulted in the production of ethane.

The data graphically presented in Figure 5 are in marked contrast to the data of Figures 1 to 4. Figure 5 presents information obtained by the co-conversion of ethylene, carbon monoxide; and hydrogen in contact with an iron catalyst containing 0.5 weight percent K at 1150 p. s. i. g. and various temperatures. The HzzCo mol ratio was about 4.8. It will be noted that maximum conversion of ethylene was obtained at temperatures between about 350 C. andab'out 425 C., under which conditions the carbon monoxide is completely converted, together with most' of the hydrogen charged to the reactor. Coincident with. maximum ethylene conversion, onlya" relatively small proportion of the ethylene is converted to ethane, and methane production islikewise'at alow level. The yield of C3 and higher hydrocarbon products rises sharply with increased ethylene conversion and, in fact, at-

4 tains a maximum over the temperature range of about 360 to 425 C.

Surprisingly, the H22CO molar conversion ratio was far in excess of that obtained with iron catalysts in the Fischer-Tropsch synthesis but the production of oxygenated compounds was quite low. The oxygen content of 1.36 weight percent in the product corresponds to about 10 weight percent of oxy compounds calculated as octanol. The present synthesis was also sharply distinguishable from the Fischer-Tropsch synthesis not only by the composition of the charging stock and operating conditions, but also by the fact that at most 1 or 2- weight percent of'water waspro-duced by the reaction, whereas in the Fischer-Tropsch synthesis it frequently happens that as much as about 50 mol percent of the oxygen content of the C0 charged is converted to water.

Figure Sis a plot of data obtained by the con version of a mixture of propylene (89 mol percent), carbon monoxide (5.3 mol percent) and hydrogen (3.8 mol percent) in the presence of an alkalized iron catalyst at 1100 p. s. i. g. and temperatures from 346 to 448 C. It will be noted that hydrogenation reactions leading to the production of propane are minimized under the conditions of maximum conversion of the propylene' and that the conversion of propylene to C4 and higher hydrocarbons closely parallels the propylene. conversion curve under conditions of maximum conversion. Essentially quantitative conversion. of carbon monoxide is obtained under conditions of maximum propylene conversion and methane production. is low and. unim portant under these conditions.

The tables below present. the experimental data; which have been graphically presentedin Figures 1 to 6.

, Polymerization oi Ethyl ene over Unalkalized Iron (Fig. 1)

Experiment Number 129 atalyst Charge, gins M Total; 1 413 413 413 Feed Charge. gms:

Eth ene 48 224 370 Carbon Monoxide 0 0 0 Hydrogen. 0 0 0 Experimentalcop ditionsz Temperature, C n- 395 535 585 Pressure, p. s. i. g l, I, 100 l, 100 S. V. gms. Feed/gm. Catalyst/hr 0.076 0.218 0.328 Conversion of Feed. weight percent 37 40 '63 Conversion ofEthylene, weight percent 37 49. 63

Conversion of" Carbon Monoxide, weight percent ch Conversion of'Hyd ogen, weight percent. Composition of Product, weight percent: Hyd ogen-..

Butanes. Pentenes and Higher Total. .1.

Composition of C5 Product weight percent:

Total Weight percent Oxygen as (0=l6)in C Percent.Unsatin-atiomC Cn-cuts Weight percent Oxygen as (O=16) in C "geno e Polymerizationoi Ethylene over Alkali'zed Iron (Fig. 2)

Experiment Number Catalyst Charge, gms:

Total Feed Charge, gms.:

Eth

Hydrogen Experimental Conditions: Temperature, C Pressure, 1). s. i. g. S. V. gms. Feed/gm. Catalyst/h Conversion of Feed, weight percent' Conversion of Ethylene, weight perce Conversion of Carbon Monoxide, weight Conversion of Hydrogen, weight percent Com osition of product, weight percent:

Hydrogen. Methane, Ethane" Propylen Propane.

Pentenes and 1g e Total Weight percent Oxygen as (0=l6) in 0 I wb t- N I zommooom 4 Percent Unsaturation C5-C9 outs Polymerization of CZHA-CO over Alkalizod Iron (Fig. 3)

Experiment Number Catalyst Charge, gms:

Iron 20 Total .L

Feed Charge, gins;

thylene Carbon Monoxide Hydrogen Experimental Conditions:

Temperature, C

Pressure, p. s. i. g S. V. gms. Feed/gm. Catalyst/hr"- Conversion of Feed, weight peroent Conversion of Ethylene, weight percent. Conversion of Carbon Monoxide, weight percent Conversion of Hydrogen, weight percent Com osition of Product, weight percent:

Hydrogen Methane Propane Bnfenpq Butanes.. Pentenes and Higher Total Composition of C Product weight percent:

Total Percent Unsaturation C C cuts low-50203300 |emsu em g eneralar lm suesu Experiment Number;

Polymerization of Propylene-Carbon Monoxice-Hydrogen Mixture over Alkallzed Iron: Catalyst (Fig. 6) I Catalyst charge g.:

Iron i 280 280 280 280. 280 Alkali (K 1.4 1.4 1.4 1.4 1.4

g Total 281. 4 281. 4 281.4 281.4 281.4 281.4

Feed Composition, weight per cent:

Hz 0.2 0.2 0.2 "0.2" s 0.2 0.2 CO. 3.8 3.8 3.8. x .3.8 3.8. 3.8 CiHt 96.0 96.0 96.0 96.0 96.0 96.0

Operating Conditions: 7 Temperature, C 346 372 391 407 .420 448 Pressure, p. s. i. g 1, 100 1, 100 1,100 1, 100 1,100 1,100 S. V. g. HC/g. Cat/hr l i 0. ll 0. 03 0. 06 0. 21 0.21 0. 28

Conversion C Hu, weight per cent 33 55 68 45 48 48 Conversion 11;, weight per cent 50 50 50 50 -50 i(-50) Conversion CO, weight per cent 90 95 54- 95 41 90 Composition of Product, weight per cent.

100 100 100 100 100 100 Composition of Combined 05+ Product, Weight per cent:

C 7 Cu 28 C1 8 Ca 9 .109 Btms 28 Total 100 1 Represents gain in Hz p 1 In the practice of our invention, we prefer to Figure 7. An olefinlc hydrocarbon, preferably 'a employ normally gaseous, non-tertiary olefins as feed stocks. We may employ mixtures of diiferent olefins and/or paraffms, such as are frequently produced in petroleum refinery operations. We may also. employ'normally liquid olefins, such as l-pentene, Z-pentene and the like, or hydrocarbon mixtures comprising normally gaseous and normally liquid olefins. Isoolefins, such as isobutylene, trimethylethylene and the like are relatively less reactive charging stocks than non-tertiary olefins. Olefinic charging stocks for the purposes of the present invention can be prepared, purified or concentrated by conventional methods which,

form no part of this invention. I 1

Although certain illustrative ranges of operating conditions have been indicated in the above specific examples, it should be understood that the conditions therein recited are not limitative of the invention. In general, the proportion of carbon monoxide plus hydrogen in the total charging stock to the process may be varied between about 5 and about 40 volume percent. The H2:C0 mol ratio may be varied between about 0.5 and about 10 and is preferably between about 1 and about5. The temperature in the conversion zone may be varied between about 350 and about 425 C., and is preferably between about 375 and about 400C. The operating pressure may vary between 250 and 2500 p. s. i. g., and is preferably maintained between about 500 and 1000 p. s. i. g. When the catalyst is employed in the form of a fixed bed, the reactants are passed therethrough at a space velocity which may be between about 0.01 and about 0.3 part by weight per hour per part of catalyst, preferably about 0.1 to about 0.2. When the catalyst is employed in the form of a fluidized powder bed, the above-mentioned space velocity can be increased by a factor of about 10. An illustrative representation of the process of our inventionis depicted in the flow diagram,

separators or filters (not shown) may be provided in the upper portion of the reactor to, separate catalyst powder entrained in the gaseous stream leaving the reactor and to return said powder to the fluidized bed in the lower part of the reactor. We may employ, for example, a fluidized solids catalytic reactor such as the one illustrated and described in U. S. Patent 2,347,682. 7

We may employ iron catalysts such as have heretofore been employed in FischereTropschhy drocarbon syntheses (note Storch, Chem. Eng. Prog. 44, June 1948, page 469; Latta and Walker; ibid, 44, February 1949, pages 173-6). Thus the catalyst may be a commercial alkalized iron such as the onecommonly employed in the conversion of nitrogen and hydrogen to ammonia, which catalyst in the unreduced state consists essentially of F6304, 2.5% alumina and 0.5% K20. We may also employ an iron catalyst promoted with iron fluoride, such as the catalyst described in U. S. application for Letters Patent S. N. 794,120 filed by Herman S. Seelig and James Zisson on'Decer'n ber 26, 1947, or an iron catalyst prepared by comminution andreduction of 'mill scale, as described and claimed in S. N. 770,749 filed by Scott w. Walker on August 26; 1947', now U. s.- Patent Number 2,485,945. Although iron is the essential or principal component of the catalysts employed in the process of the present invention, it should be understood that other metals, which-mayor may not exert catalytic efiectsmaybe present in the catalysts. Thus the catalysts may contain minor proportions, usually betweenabout 0.1 and about 25 percent by weight of one or more metals other than iron, e. g. copper, cobalt, thorium, manganese, vanadium, etc. The catalyst may be supported on alumina, silica, kieselguhr, acidtreated clays or the like. Alkali metal salts, especially fluorides, or their oxides r carbonates may be employed in amounts between about 0.1 and about 5 weight percent based on the iron to promote the catalyst. The promoters may be added to the iron catalyst not only in the course of preparation but also during the synthesis. The catalyst may be reduced in situ in the reactor.

The catalyst powder may have a particle size between about 100 and 400 mesh and a bulk density between about and 100 pounds or even more per cubic foot in the fluidized condition. Fluidization of the catalyst bed in the reactor is obtained by passing the reactants in the vapor phase therethrough at a vertical vapor velocity between about 0.1 and about 10 feetper second, preferably between about 0.5 and about 2.5 feet per second. Y

A mixture of carbon monoxide and hydrogen is added to the olefin charging stock through valved lines I5 and 38. The carbon monoxide-hydrogen stream is blended with the olefin charging stock to produce a mixture containing between about 5 and about 40 volume percent of carbon monoxide and hydrogen, for example, about to about volume percent carbon monoxide and hydrogen. The mol ratio of HzICO charged to the reactor maybe varied between about 0.5 and 10 or even more and may suitably be about 3 toabout 5.

A suitable method for producing a mixture of ethylene and/or, propylene with carbonmonoxide andhydrogen comprises oxidative dehydrogenation or cracking .of gas mixtures containing ethane and/or propane, essentially as practiced in Germany (PQB. Report 52,854'byM. A. 'Matthews). Theiprocedure consists of preheating the hydrocarbongas stream to 6504580 (3., mixing it with oxygenpreheated to 450-550 C., using'0L4 to 0.5 mol-oi oxygen per mol of hydrocarbon, andpassingthe mixture through aspecial refractory ceramic reactor at an absolute pressure of 320-360 mm. of mercury. The mixtures of olefins, carbon monoxide and hydrogen thus produced can be blended with further quantities of olefins, if desired, and charged to the present process. Part ofthe tail gas from the polymerization or conversion operation can be recycledlto the oxidative dehydrogenation process.

The reaction which occurs in reactor 13 is highly exothermic. Heat .removal may be effected from the reaction .zone by the employment of cooling tubes or coils disposed in the dense phase fluidized catalyst bed. The-heat removal facilities depicted in Figure '1 comprise a waste steam boiler Hi to which water is charged through valved line H, passed through valved line 18, through coils or tubes l9 disposed in the dense fluidized catalyst bed, thence through valved line 20 to boiler or steam separating drum Hi, from which steam is vented'through line 2| under controlled pressure.

An aliquot portion of the catalyst maybe withdrawn intermittently or continuously through valved'line 22 to pass into a regenerator schematically depicted by 23, whenc regenerated catalyst passes through valved line 24 :and cooler 25 back to the lower portion of the dense phase fluidiaed-catalyst-bedin reactor I3. Spent-catathrough valved line 21.

The regeneration procedures employed are those which have heretofore been employed for r the regeneration or reactivation'of iron Fischer- Tropsch catalysts and comprise principally treatment with hydrogen, alternate oxidation and reduction of the spent catalyst, extraction of the spent catalyst with wax solvents, etc.

The vapor-ous or gaseous charging stock is treated in reactor 13 at a temperature between about 350 and about 450 0., usually at a temperature between 375 and 425 (3., and Pressures between about 250 and 3000 p. .s. -i. g., usually about Z50 to 1500p. s. i. g. Upon completion of the desired reaction period, the converted stream is passed from the upper portion of reactor l3 through line 28'and pressure reducing valve29. thence through partial condenser '30 into aseparating drum 3!.

Suitable conditions to be maintained in .separator 31 include a temperature-between-about 20 C. and about 50 C., and a pressure of about to about 1000 p. s. i. g. Liquid conversion products are withdrawn from the lower portion of separator 31 through valved line 32 and maybe subjected to'aftertreatment as hereinafter described. Gaseous products are discharged from the separator-3l through valved line33 and are passed to a zone 34 in which they are treated to recover normally liquid hydrocarbon conversion products entrained in the gas stream. Zone 34 may take the form of an absorber or fractionatin column and is depicted in the latter form in Figure '7. A reboiler coil 35 is provided in the lower portion of tower 34. Ages stream comprisingprincipally carbon monoxide and hydrogen, which may also include varying amounts ofmetlrane, ethane, ethylene and Cahydrocarbons, is discharged from the upperend oitower 34 through line 36 whence all or analiquot portion may :be discharged from the system throughvalved line 31, or all or a part of said stream maybe passed through valved line 38 to join the olefinic charging stock passing through valvedline l0 into reactor 13. A side-cut consisting essentially of unconverted olefin may be trapped at an intermediate zone in tower '34 and partially or wholly discharged from the system through valved line 39. It is preferred that at least a portion of the unconverted olefin withdrawn fromthe tower 34 be recycled through valved line I2 to reactor I3 for conversion. Hydrocarbon'converslon productscontaining a greater number of carbon atoms per molecule than the olefinic feed stock'are withdrawn from the lower end of tower 34 through valved line 40, whence they are passed to'valved line '32 to join'the, primary stream of hydrocarbon conversion products withdrawn .from separator 3|.

Although Figure 7 depicts a fluidized catalyst system for the conversion of olefins, carbon'monoxide and hydrogen, it will be apparent that the present process is not restricted to the employment of the catalyst in the fluidized .powdered form. Thus, we may employ a fixed bed of irontype catalyst; a fixed .catalyst'bed was utilized in carrying out. the experiments which yielded the data tabulated above. Other methodsof contacting catalysts and the reactants are known'in the art and may be used vfor the purposes of the present invention. Thus, we may pass the reactants upwardly against a downfiowingstream hydrocarbon'oil, withdrawing a portion of the slurry from time to time to separate synthesized products and catalyst. The catalyst may'also be maintained as a stationary bed of pellets through which the liquid or liquefied olefin charging stock, or-a solution of olefin charging stock in a suitable oil, is passed downwardly against a rising stream or carbon monoxide and hydrogen. -In lieu of employing a fluidized fixed bed ofpowdered catalyst, we may blow a suspension-of reactant vapors or gases and powdered catalysts through the reaction space, employing a're'actor of the general type described and illustrated in U. S. Patent 1,799,858.

It will also be evident that in lieu of employ-- ing one reaction zone We may employ 'a plurality of reaction zones through which the reactants are passed in parallel, series ors'eries-parallel, with intermediate separation of synthesized productsfrom the reactant streams between passes through the reaction'zones. I

The hydrocarbon products produced'by the process of the present invention contain a substantial proportion of mono-olefinic hydrocarbons. As the abovetabulation indicates, the C5-C9 fraction may contain-about to 70% of mono-olefinic hydrocarbons. In the polymerization of ethylene, propylene, 1- or 2-butenes or their mixtures, straight chain l-olefin hydrocarbons form a substantial proportion of the polymer product. Acid-catalyzed polymerization, especially of propylene or but'ylenes, normally leads to the production of branched-chain polymers. It is also noteworthy'that the conversion of 'eth-' ylene by the present process yielded only small proportions of dimer under the selected condi-' tions and substantial yields of :trimer and tet ramer.

The hydrocarbon conversion product of the present invention may besubjected to a-variety of aftertreatments' or conversion operations.

The hydrocarbon product is customarilyFdistilled to separate fractions of. desiredboilin range and unsaturat-ion. Arelatively small proportion of water and oxy compounds contained in the hy-. drocarbon product may be removed by treatment of the product with suitable adsorbent materials such as activated carbon, silica gel, acid-treated clays or the like, optionallyin the vapor phase,

as, in the treatment oi Fischer-Tropsch -hydrocarbon products containin oxygenated organic compounds. The hydrocarbon products of the present invention may also be subjected to contact with alkaline earth metal oxides at high temperatures, for example from about 100 to about 300 C.,.in order to dehydrate oxy compounds contained in said product and to increase the yield of hydrocarbons, especially olefins', derivable from the present process- Since the olefinic. products produced by our invention, especially by. the. treatment of normally gaseous non-tertiary olefins, boil substantially Within the boiling range of gasoline and comprise a substantial proportion of straight-chain l-olefin hydrocarbons, they are especially valuable starting materials for the preparation of synthetic lubricating oils and diesel engine fuels- The products :of our invention or unsaturatedw fractions thereof boiling within the gasoline boiling range may be .subjected to polymerization,

which are highly. useful as. highespeed, diesel;

engine fuels; Stronger acidxcatalystsisuch as, aluminum chloride, HF and HF-j-BFymay, be used to produce synthetic polymers-which are suitable for use as-iubricating oils. Suitable polymerization processes, 'forexample, are those which have been described in U. S. Patent 2,079,857 of Vanderveer Voorhees, whichissued May 11; 1937. Other suitable polymerization procedures employingaluminum chloride as a catalyst, and naphtha :as-the diluent have been described by F. W. Sullivan, Jr.,, V.= Voorhe es A. W. :Neeley and R... V..,Shankland 'i-n- Ind. Eng.- Chem. 23,604 (1931);

We. have observed that the polymerization of l-octene with 2.6 weight percent, of BF3 for 105 minutes at 57 F. producedweightpercent of polymer, 96 percent by, weight ofwhich-boiled within the diesel fuel boiling range. The trimer fraction of this polymer had a cetane number of 64. Hydrogenation of the polymer yieldedhydrotrimers having a ,cetane number of 76 and hy,-

drodimers and hydrotetramers having a cetane;

process of the present invention into synthetic,-

lubricating oils and diesel engine fuels ,it will be appreciated that the utility of thev present products is not thus limited; It will be apparent thatthe olefinic and ,paraffinic hydrocarbons produced by the present, process are suitable charg ing stocks for numerous chemical conversions to;- produce derivatives such as alcohols, ketones, esters and the like. Acidic catalysts effect poly--. merization of the straight-chain, gasoline boiling range mono-olefinic hydrocarbons,=-derived from the conversion of normally gaseous, non-tertiary; mono-olefins, carbon monoxide and hydrogen with iron catalysts as herein described, to dimers and trimers containing between about 12 and about 16 carbon atoms, which may besulfonated with strong sulfuric acid, chlorosulfonic acid, or other halogensulfonic acids to produce straightchain alkyl sulfonates which areof great-value assynthetic detergents and wetting agents. Al'-.. ternatively, the olefinic combination of iron-catalyzed and acid-catalyzed polymerization processes may be employed for the. alkylation of aromatic hydrocarbons, particularly-benzene, toluene, xylenes, ethylbenzene or the like, .tt'i product' mono-alkylates' which upon sulfonation and neutralization with caustic or the like yield valuable alkylaryl sulfonates.

Having thus described our invention what we claim is:

1. A process for the conversion of an olefin,

products preparedzby the 

1. A PROCESS FOR THE CONVERSION OF AN OLEFIN, CARBON MONOXIDE AND HYDROGEN TO A HYDROCARBON CONTAINING MORE CARBON ATOMS PER MOLECULE THAN SAID OLEFIN, WHICH PROCESS COMPRISES CONTACTING A FEED STOCK COMPRISING SAID OLEFIN AND BETWEEN ABOUT 5 AND ABOUT 40 PERCENT BY VOLUME OF A MIXTURE OF HYDROGEN AND CARBON MONOXIDE HAVING A MOL RATIO OF HYDROGEN TO CARBON MONOXIDE BETWEEN ABOUT 0.5 AND ABOUT 10 WITH AN ALKALIPROMOTED IRON CATALYST AT A TEMPERATURE BETWEEN ABOUT 350* C. AND ABOUT 425* C., AND A PRESSURE 